Apparatus for the treatment of water solutions by ion exchange

ABSTRACT

Treatment of watery solutions by means of ion exchange; the exchange mass through which the liquid under treatment flows is conducted from a bottom funnel of the treatment container to a regenerating-and-wash-column and thence back to the liquid treatment container. After leaving the liquid treatment container and before entering the regenerating-and-wash-column the ion exchange masses are back-rinsed in a back-rinse container; the ion exchange mass is transported from the regenerating-and-washcolumn means of an immersion tube at the top of the regeneratingand-wash-column, the depth of immersion of the immersion tube being adjustable according to the volume in the bottom funnel of the treatment container; consequently the ion exchange mass in the head of the regenerating-and-wash-column which has been transported from the treatment container corresponds to the volume transported from the bottom funnel thereof.

United States Patent 11 1 1111 3,915,861

Marquardt 1 Oct. 28, 1975 1 APPARATUS FOR THE TREATMENT OF 3.193.4987/1965 P1111181 et 11 210/33 WATER SOLUTIONS BY ION EXCHANGE 3.554.3761/1971) Kunz 210/189 3.619.425 11/1971 13111111 e1 111 210/33 [75]Inventor: -Kurt Paul Marquardt,

Holzgerlingen. Germany [73] Assignee: Hager & Elsaesser,

Stuttgart-Vaihingen. Germany [22] Filed: Sept. 10, 1973 [21] Appl. No:395.854

Related U.S. Application Data Primary fixuminer Thomas G. Wysc 1571ABSTRACT Treatment of watery solutions by means of ion exchange; theexchange mass through which the liquid under treatment flows isconducted from a bottom funnel of the treatment container to aregeneratingand-wash-column and thence back to the liquid treatmentcontainerv After leaving the liquid treatment container and beforeentering the regenerating-andwash-column the ion exchange masses areback-rinsed in a back-rinse container; the ion exchange mass istransported from the regenerating-and-wash-column means of an immersiontube at the top of the regenerating-and-wash-column, the depth ofimmersion of the immersion tube being adjustable according to the volumein the bottom funnel of the treatment container; consequently the ionexchange mass in the head of the regenerating-and-wash-column which hasbeen transported from the treatment container corresponds to the volumetransported from the bottom funnel thereof.

6 Claims, Drawing Figures [63] Continuation of Ser. No. 135.146, April19. 1971,

abandoned.

[30] Foreign Application Priority Data Apr. 17, 1970 Germany 2018455June 16, 1970 Germany 2029720 [52] US. Cl 210/189; 210/268 [51] Int. Cl.BOlj 1/06; B01d /04 [58] Field of Search 210/25, 30, 33-35, 210/189,248, 268, 291-293 [56] References Cited UNITED STATES PATENTS 2,422,0546/1947 Tiger 210/25 2,767,140 10/1956 Fitch 210/33 3,019,079 11/1962Donohue 210/33 X US. Patent Oct.28, 1975 Sheet10f6 3,915,861

firm/0r.- BYKURT PAUL MARQUAR ATTORNEY U.S. Patent Oct. 28, 1975Sheet20f6 3,915,861

Wenfor: KURT PAUL. MARQ QRDT TToKNEY U.S. Patent Oct. 28, 1975 Sheet30f63,915,861

Imp/0r.- KURT PAUL MARQUARDT ATTORNEY US. Patent Oct.28, 1975 Sheet5of63,915,861

N //W.4/7f0r: B KURT Pam. MARQUARDT A TTORNEI U.S. Patent Oct. 28, 1975Sheet 6 of 6 lrWe/rfar: Kurt Paul MARQUARDT Attorney APPARATUS FOR THETREATMENT OF WATER SOLUTIONS BY ION EXCHANGE This is a continuation ofapplication Ser. No.

l35,l46, filed Apr. 19. 1971, now abandoned.

This invention relates to an apparatus for the treatment of waterysolutions by means of ion exchanges. Such treatment may involve. forexample. the preparation, softening. and/or the desalinating of suchsolutions. The ion exchange mass. through which the liquid to be treatedflows, is conducted through a treatment container in which it contactsthe liquid being treated. and thence to aregenerating-and-washing-column from which it is returned to thetreatment container.

There are already known a number ofdifferent types of installations forcarrying out the liquid treatment in a continuous or a quasi-continuousmanner, wherein the necessary processes for operating the ion-exchangefilters, such as exchange, rinsing-and-regenerating the ion exchangemass. etc. are not carried out in one tank, but successively indifferent apparatus within one cycle. These installations, in contrastto the operation of the so-called fixed-bed filters, wherein thebackrinsing, regeneration and washing of the ion-exchange mass iscarried out after loading in the same, one tank, have the advantage thatduring the regeneration practically no interruption of the working cycleoccurs. With classical procedures, on the other hand, it is necessary toinsert a spare filter during the down-time ofthe main filter. This isnot necessary with a constantly working circulating process wherein theprocess steps for the treatment of the water as well as the regenerationof loaded ionexchange mass take place simultaneously.

A quasi-continuous process for operating ionexchange filters has alreadybeen proposed, wherein the regenerating and washing of the exchangemasses takes place in one tank. Specifically, the regeneration takesplace in a lower part of a regenerating-andwashing-column, thepre-washing takes place in a middle part of such column, and the clearwashing takes place in the upper part of the column. However, it hasbeen found that with very dirty liquids such as a cleaning process inwhich the regenerating is also carried out in the same, one tank, suchregeneration is not sufficient. The resins are not sufficientlyloosened, so that the particles and the dirt clinging to the resin willnot be washed out thoroughly enough. Because of this, the resistance ofthe filter to liquid flow increases and the total efficiency of theconstruction progressively decreases.

Among the objects of the present invention is the creation of aneconomical apparatus for the quasicontinuous treatment of liquids byion-exchange masses, in a cycle wherein such ion exchange masses areconducted through a processing tank and aregenerating-and-washing-column. In accordance with the presentinvention the ion-exchange masses are thoroughly rinsed, and theprocess, in comparison to the traditional or classical processes, iscarried out with little expense and with a greater security.

In accordance with the present invention, the ionexchange masses leavethe liquid processing tank through a bottom funnel, and before enteringthe regenerating-and-washing-column flow into a rinsing tank in whichthey are thoroughly re-rinsed at least once during each entire cycle.The removal of the ionexchange masses from the rinsing tank and from therege neratingmnd-washing-column is effected by means of headpieccscarrying submerged tubes extending into the inner tank. The volume ofthe headpieces is determined with respect to the volume of the outletfunnel by \arying the submerged depth ofthc immersion tubes as required.The ion-exchange masses located in the head of the tank and extending tothe level of the submerged depth of the immersion tubes corresponds toone portion. As will be explained later on, it is possible with thisprocess to treat very polluted liquids simply and thoroughly. Thesubmerged or immersion tubes, in which the leaving and to be transportedresin is intro duced and taken off. respectively. as the transportingwater is introduced via the head of the tank is inserted and drained,respectively, provide a simple determina tion ofthe portion ofthe resinto be transported as well as a simpler and surer transport of suchresin. If the tanks are filled, water accumulates in the submergedpipes. so that at the introduction of the transport of resin there isfirst moved water which is mixed with the first exchange particles.Consequently, there will be predominantly water at the beginning of thetransport, which will ensure a good transport security.

The installation of the invention works with great advantage underconditions in which the interval between the beginnings of successiveworking cycles, in which the ion exchange masses are taken off andtransported (working time) is at least 8 minutes.

The apparatus of the invention can be used with the same advantages,without additional construction costs, in a mixed-bed type ofinstallation. It is, consequently, not limited to applications in whichthe working tank contains only cation-exchange masses or anion-exchangemasses. In such a case, according to the invention, by employingmixed-bed ion-exchange masses in the re-rinse tank there occursimultaneously in the tank a separation of the cation and the anionexchange masses, which are taken off from the re-rinse tank separately andat different levels for washing and regenerating, and are transportedinto separate tanks and from there, after mixing, are returned to amixedbed treating tank.

To obtain a good degree of cleanliness of the liquid which has beentreated and a total utilization of the regenerating means, in theapparatus of the invention it is provided that the regenerating means atthe point of entrance thereof be provided with an impacting and dilutingmeans which provides for a transverse water flow. To prevent a counterion effect there is provided, for a successful continuation of theprocess, means whereby at the standstill of the pure water take-off thethen-stored pure water overflows into the raw water storage tank, byway, for example, of the raw water conduit.

Further advantages and characteristics of the invention will becomeapparent from the following description and the accompanying drawings,wherein there are shown several embodiments of the apparatus inaccordance with the invention.

IN THE DRAWINGS:

FIG. 1 is a circuit diagram of a quasi-continuous working fulldesalination plant according to the invention, comprising by way ofexample a twostage plant;

FIGS. 2, 3, 4, and 5 are schematic reproductions of a part of the plant,such figures demonstrating the process in different stages of thedesalination process;

FIG. 6 is a view in horizontal cross-section through the flange piecedisposed between the regenerating and the washing zones of theregeneration-and-washcolumn;

FIG. 7 is a view in vertical cross-section through the flange piece, thesection being taken along the broken section line 77 of FIG. 6;

FIG. 8 is a portion of a circuit of the mixing bed according to theinvention;

FIG. 9 is a part of the circuit of a so-callcd shock rinseinstallation"; and

FIG. 10 is a view in side elevation of a modified arrangement of aback-rinse regenerator-and-washcolumn.

In the schematically represented circuit of FIG. 1 there is shown aquasi-continuous working installation for treatment of liquid agents. Tosimplify matters, the following description is that of the treatment ofwater.

The circuit shown is a two-stage installation in which the water to betreated flows through two treatment or operating containers, onedesignated K, which is a treatment-container 21 holding cations, thesecond stage, at the left, being a treatmentcontainer A filled withanions. The two stages are exactly the same; the following descriptionis mainly concerned with the right hand part of the installation asshown in FIG. 1, in which the cation-exchanger is located.

The untreated water is fed by means of a pump 40 from an untreated watercontainer 48 via a conduit into the treatment container 21. Thethroughflow, which is indicated by means of a flow through volume meter50, which is located in front of a back-shockvalve 51, is regulated bymeans of a valve 1 disposed in the conduit 20. There is present in thecontainer 21 ion-exchange mass 22 through which untreated water flows ina direction from the bottom to the top of the container. The clean waterleaves container 21 by means of a valve 2 which adjusts the rate of flowof the liquid through the discharge conduit 24. Immediately in advanceof the entrance to container 21 there is provided a branch 20a with avalve 7 in the untreated water conduit 20.

At the bottom of container 21 there is a funnelshaped collecting chamber21a which is connected by means of a conduit 25 provided with a valve 4with a return-rinse container 31. Connected to this conduit 25 through avalve 14 is another conduit 45 which feeds transport-and-return-rinsewater from a clean water container 49 by means of a pump 47. A conduit27, in which there is interposed a valve 9, is branched off con duit 45and leads to the upper end of the return-rinsecontainer 31. A rinseconduit 32 is also connected to the top of the return-rinse container31, conduit 32 having an adjustable valve 11 interposed therein. A dirtywater tube 34, which is selectively sealable by a valve 8, is connectedto the container 31 somewhat below the top thereof. The bottom of theregenerating container 41 is connected to the top of the return rinsecontainer 31 by means of a conduit 36 in which there is interposed acontrolable valve 5. The regenerating agent is introduced through aconduit 46 and a valve 52, conduit 46 being attached to the middle partof the column 41 as shown. A circulating tube and pump 17 is provided inthis region, the pump being connected in a loop composed of conduitportions 64, 18, and 63. See FIGS. 6 and 7 as to the location of theconduit portions 63, 64.

To the bottom of column 41 there is attached a drain tube 38 having avalve 13 interposed therein. The drain tube 38 has a ventilation conduit39 secured thereto. In

advance of the valve 13 there is provided a tap l5 and also the branchofa drain tube 16 provided with a valve 19. Diluting water is fed overthe head of the column 41 by way of a tube 42 having a then adjustablevalve 12 therein, the conduit 45 being connected to conduit 42 through avalve 6. To the upper region of column 41 there is attached atransmission tube 43 having an adjustable valve 3 interposed therein,and a further, drain tube 44 which is adjustable by means of a valve 10,the conduit or tube 43 leading to the top of the treating container 21through the valve 3. Connected to the container 21 at different levelsthere are a plurality of taps 5356, inclusive, for taking off watersamples to measure the output capacity of the installation.

The above-described installation operates in the following manner:

As stated above, the installation is quasicontinuously working, thefeeding or transport of the ion-exchange masses taking place cyclicly.Such masses may be fed constantly by means of a time-relay whichoperates at intervals, or it may operate at discontinuous intervals ifthe interruption time is controlled by a measured value, for example,when a definite value of conduction capacity is reached, which isdependent on the degree of exhaustion of the ion exchange masses in thecontainers A and K. The water-conducting valve 6 is opened in order tofeed freshly-regenerated ionexchange resins from thewashing-and-regeneratingcolumn 41 into the top of the treating container21 through the conduit 43 and the valve 3. In such operation the valve 2will have been closed, the untreated water conduit 20 will have beenclosed by shutting valve 1, and valve 7 in conduit 20a will have beenopened so as to drain the untreated water in container 21 into areservoir (not shown) for re-use.

After a short interruption, in order to accomplish the described feedingof the ion-exchange mass, the valve 1 in the untreated water conduit 20and the valve 2 in the clean-water conduit 24 are re-opened. In the nextcycle, the loaded ion-exchange masses 22 which are located in the drainfunnel 21a of the container 21 are, by brief openings of valves 4 and11, fed through the conduit 25 into the back-rinse container 31. Afterthis, valve 14 is opened for supplying transport and returnrinse waterto the container 31. A portion of the resin still present in the returnrinse container 31 is conducted, with valves 5, 9, and 10 open, into thewashingand-regenerating-column 41.

After this, the return-rinse action in the return-rinse container 31takes place. The rinse water is led into the bottom of such containerthrough valve 14 and conduit 25, while the dirty water is drainedthrough conduit 34 and open valve 8. At this time the valves 9 and 11are closed. Simultaneously with the regeneration of backrinse water theion exchange masses located in the washing-and-regenerating-column 41will be regenerated. The regenerating agent is fed into column 41through open valve 52 and is led over back-washed resin located incontainer 31, while diluted water is being conducted through tube 42 andopen valve 12 into the top of the regenerator container 41. The usedregenerating agent is drained from container 41 through tube 38 andopened valve 13. The drainage of transporting water is effected throughtube 44 and opened valve 10 during the influx olthe backflow ofion-exchange portions into the container 41.

The clean water flowing from the top ofcontainer 21 through conduit 24is fed to anion container A and leaves the latter through clean-watertube 30. Lye for regenerating the ions is fed through a conduit 57 tothe regenerating container at the left in FIG. 1. The operation of theabove-described process will be better understood upon consideration ofFIGS. 2-5, inclusive. In such figures the same parts are designated withthe same reference characters as those employed in FIG. 1. In FIGS. 2-5,inclusive, there is shown a treatment container 21, a backflow rinsecontainer 31, and a regeneratingand-washing-column 41. In order toprovide a greater length of column 41, as shown in FIGS. 2-5, inclusive,such column is of U-shape. As a result of such construction, much spaceis saved.

As shown in FIGS. 25, inclusive, the ionexchange masses are drained fromcontainer 31 and 41 by means of immersion tubes 23 and 33 respectively,such tubes being submerged in the container headpieces to a depth suchthat just one resin portion can be drained in one cycle of the operationof the installation. In this manner, there is always possible a simpledetermination of the transported resin, which is that amount in the headof the column which can be drained through the tube up to the level ofimmersion of the tube. The resin portion formed by the depth ofimmersion of the tubes 23 and 33 corresponds to that amount in the drainfunnel 21a of container 21. These volumes must be coordinated.

The use of the immersion tubes 23 and 33 has, apart from the simpledetermination of the resin portion to be forwarded, the additionalessential advantage in comparison with all of the other wellknownmethods of this kind: the forwarding of the resin portions isinterrupted only by the time interval of the opening and closing timesof the valve. When a minor water push follows the transport or feedingof the resin, the feeding conduits are rinsed clean and no residue ofresin will be present in the tubes and valves. In this manner, thewearing of the valves and the wasting of resin are avoided.

In FIG. 2 there is illustrated a condition wherein there occurs aforwarding of the ion-exchange mass from container 21 through conduit25, with valve 4 open, into the back-rinse container 31. In such figurethe valves which are open are illustrated with an outline only whereasthe valves that are closed are shown fully inked-in. A part of thepartially drawn resin is already in the lower funnel part 310 of theback-rinse container 31, while a further, already used, resin portion31a is settled over a mixing zone 31b. In order to obtain a thoroughrinsing of the resin, the volume of container 31 is calculated to beable to contain at least two resin portions.

During the back-rinse process, the washing-andregenerating process takesplace in the washing-andregeneratingcolumn 41 in different zones thereofwhich are marked accordingly. The regenerating agent is fed throughconduit 46 in the middle region of column 41, and the resin introducedthrough conduit 36 is regenerated in the eountercurrent. In this waythere are obtained three zones corresponding to the time of stay of theresins during three working cycles. In the re gion 41a, in which theresin is in contact with the used regenerating agent, there takes placea preregeneration. In region 41b regeneration takes place; in region 410the resin is in contact with the concentrated, unused regeneratingagent. In order to achieve a uniform regeneration at the influx. aconstant circulation is provided by a conduit 46 to which the conduit 18is connected, the pump 17, described in detail in connection with FIGS.6 and 7, and the conduit 64. In the region 41d, 4le. and 41fthenewlyregenerated resin is washed. The wash and diluting water is fed inthrough conduit 42. The water flowing through resin portion 412 (in thewash zone) which is still rather relatively clean. prewashes the resinin region 41d. In the regenerating zones this water simultaneouslyserves as diluting water, so that an optimal use of the water ispossible, which has favorable effects on the water consumption and thevolume of water to be drained. The water entering zone 41e from zone 41dstill contains an excess of regenerating agent, which, together with theregenerating agent fed. are used completely, so that consumption ofregenerating agent is very small.

In FIG. 3 there is shown the same portion of the installation as in FIG.2 but in a later portion of the operating cycle. Resin is beingtransported from back-rinse container 31 through open valve 5 to thewashing-andregenerating-column 41. A part of the washed resin 31a hasalready been drained and is located in region 41a. In the region of theclean wash zone 4f there has now occurred an accumulation of a resinportion. The displacing water is being drained through open valve 10 tothe untreated water container 48.

FIG. 4 shows the portion of the installation shown in FIGS. 2 and 3, butin the condition of baekrinsing. With valve 14 open, wash water isconducted through conduit 25, while the used rinsing water is beingdrained through conduit 34in which the valve 8 is open. There is onlyone portion of resin 31a present in the backrinse container 31, which isbeing loosened by the back-rinse and thus practically takes up the wholevol ume of the container. There are 6 portions present in 6 zones in thewashing-and-regencrating-column 41, namely, in the three regeneratingzones mentioned above as well as in the clean wash zone 41f, the washzone 4le, and the pre-wash zone 41d. Regenerating agent is fed into theregion 410, and, after passing through the preregenerator zones 41d and41a is drained through conduit 38 and open valve 13, while wash water isled in through conduit 42.

In FIG. 5 there is illustrated the flowing of resin from thewashing-and-regenerating-column 41 to the container 21 through conduit43 and open valve 3. Through conduit 42 and open valve 12 forwardingwater is being fed in, such water causing the resin to be drainedthrough conduit 33. With the inflowing of the resin portion through thehead of container 21, part of the used resin sinks to the drain funnel2la(See FIG. 1). The untreated water supply is blocked by the closing ofvalve 1, and the operation is interrupted during this short phase. Theraw water in container 21 is drained through open valve 7 in conduit20a.

As shown in FIG. 5, the upper level in container 21 is not even, but isconically shaped. This results in the first advantage, that the freefilter surface is increased, which is very advantageous at great speedsof flow in view of the self-resistance. A second advantage is that,likewise as shown in FIG. 5, a uniform distribution of the ion-exchangematerial is obtained in the operating column 21.

The different zones shown in container 21 show different grades ofloading of resin. The most strongly bonded ions, for example, Cu, Ni,Cr, Al, etc. settle in the lowest zone in the region of theuntreated-water inlet, while in the second zone, for instance Na, K, NHAg, etc. will be found and in the third zone there will be found, forexample, Na. As the heavily loaded, lowest layer is drained immediatelyto the back-rinsingand-regenerating-column 31 through conduit 25, theattack by strongly oxidizing substances on the ionexchange resins willnot be so disadvantageous as with the usual processes with ionexchangecolumns. This follows because these substances in the followingbackrinse-regenerator-exchange process are immediately again exchanged.Tensides (surface active substances) are mainly taken from the lowestlayers of the resins in the operating container 21 and are immediatelyexpelled on the next cycle. The dangerous ageing of tensides ofion-exchange substances is therefore avoided.

The degree of cleanliness of samples taken from the various taps 5356,inclusive (FIG. 1), is dependent upon the degree of loading of theresin. As soon as a proposed value of cleanliness is attained, the cycleis terminated and the resin is automatically forwarded asabove-described. The installation is designed for a min imal cycle timeof 8 minutes. With decreasing salt content of the water, the loadingzone in the operating container 21 travels downwardly, whereby the cyclenot only exceeds minutes, but, for example, will consume as much as tominutes or even more.

If no water is taken from the pipe 30 by a consumer, the clean waterwill be passed into the clean-water container 49 which is combined withthe untreated water container 48. The clean water then flows fromreservoir 49 into untreated-water reservoir 48 and from there passesthrough the untreated-water conduit 20 to the operation and treatmentcontainer 21. Since during this time there is no flow of water from thewash column 41 through the treatment column 21, the run-off from theregenerating column 41, which is not now loaded with salts, is conductedvia the conduit 38 to the raw-water container 48 after reaching thepredetermined degree of cleanliness which is determined through thetaking of samples at the tap 15. This constant turnover is advantageousto avoid a counter-ioneffect as well as to avoid a loss of ions from thecontainer 21.

The wash and back-wash water drained from the tubes 20a, 32 and 16 willbe fed to raw water container 48, while the forwarding waters, forexample, from conduit 44, will be returned to the circulation, namely inback-rinse-waterwash container 31 or in the regenerator-and-wash-column41. The used water from conduit 38 is employed only as diluting waterfor the regeneration of the chemicals. Desalinated water from theclean-water container 49 is used entirely for the forwarding of resin.The washing water is used 3 times in the regenerator-and-wash-column 41,namely to clean-wash, to wash and to pre-wash, and afterwards to be usedas a diluent in the regenerating process. Because of this, the amount ofwater needed in the process can be quite limited, which is an economicadvantage. The water consumption in this installation is considerablyless than that in other conventional installa tions having ion-exchangecolumns. The same is true for the necessary supply of ion-exchangematerials,

which are lower in this process than in other known installations.

Because of the thorough washing of resin in the backrinse container 31before the regeneration step. all types of mechanical pollution areavoided. Any finelydivided particles produced by the forwarding of theresin will be rinsed out. Water entering the system may be dosed with asuitable disinfectant material, for example, at the back-rinse container31, so as to produce disinfection of the resin.

The resin portion forwarded in one cycle of operation of theinstallation corresponds at a maximum to about 1/12 of the total volumeof the ionexchange material in the operating column 21. For theregeneration and washing process there are required the followingapproximate times:

a. with a cycle of 20 minutes in the washing-and regenerating-columnevery min.

b. with a cycle of 15 minutes in the washing-andregenerating'columnevery 45 min. An increase in the cycle volume in the wash as well as theregenerating zone leads to a predictable increase in the efficiency ofthe process and a decrease in water consumption.

As has been shown in FIGS. 1-5, inclusive, there is provided at thejunction between the wash-andregenerating zones of the regeneratorcolumn 41 a circulation conduit 18, 63, 64 in which a pressure pump 17is interposed. This junction is shown in detail in FIGS. 6 and 7. Theregenerating chemical fed through tube 46 is impinged upon by atransverse flow of a small amount of water, which occurs in a flange orcircular piece designated 60. In a circleshaped outer flange 61 there isdisposed a ring 62, which is connected with a flange through aseparating piece 65. The inner ring 62 has openings 62a therethrough, sothat the water entering through conduit 63 through opening 62a flows inthe direction of the arrows to the inner space within the ring 62 andleaves through the diametrically opposite opening 62b and conduit 64. Afine screen 66 covering openings 62a and 62b and mounted in the innerlining of ring 62 prevents the discharge of resin. Through thistransverse flow the regenerating agent is constantly acted uponthroughout the whole diameter of the ring 62. By reason of this motionof the two liquids which impinge upon each other, the regeneratortreatment is constantly diluted and simultaneously evenly distributed.Highly concentrated chemicals can be used, for example, 30% hydrochloricacid or 50% soda lye (caustic soda solution).

In FIG. 8 there is schematically illustrated a continuously-operatinginstallation in accordance with the in vention, such installationoperating as a mixed-bed installation. Parts in FIG. 8 which are thesame as those in FIGS. 1-7, inclusive, are designated by the samereference characters. In the treatment container 21 of FIG. 8 there is amixed bed, which is cycle-and-portionwise moved through a followingbackrinse and separating container 131. In this container the resinswill be back-washed thoroughly, and they thereby separate according totheir specific gravities. The cations will be drawn off by means of animmersion tube 131c in the bottom of the separating container, while theanionexchanger will be drawn off through an upper immersion tube l31b.The chamber 131a is available as an additional loosening space. As thecations will be regenerated and then washed in a post or afterconnectedwash and regenerating column 71, the anions will be fed in acorresponding rcgenerating-and-wash column 72. These columns may be ofthe same construction as those described in connection with FIGS. 6 and7. After the transporting of resins from the regeneratingand-wash column71 and 72, the resins will be reunited in a mixing piece 73 and fedthrough a conduit 43 to the container 21. The mixing piece is soconstructed that the anion and cation charges are intimately mixed andthen reach the treatment container as a mixed bed again. Thusinstallations in accordance with the invention may, without appreciablechanges, and with equal advantages, be employed for the preparation ofwatery solutions in a mixing bed with circulation flow.

It was shown that with quasi-continuous working installations asignificant disturbance may occur, by reason of considerable resistancein the upper distribution system of the treatment container 21 due topollution by fine grains, for example, abraded pieces of resin and soforth. According to the invention, a so-called shockrinsing is provided.This occurs during the short interruption phases immediately before theinflux of resin through the head of treatment container 21 with awaterflow counter to clean waterflow from top to bottom in the operatingcontainer 21, which results in the elimination of particles of dirt.Such a shock-rinse-device" is schematically shown in FIG. 9. From therinsewater tube there is provided a branch tube 80 parallel to the valve2, to be operated by a valve 81. The water necessary for this operationwill be pumped from a cleanwater reservoir 49 by means of a pump 47,which also forwards transport water via rinse-and-transport-water tube84 into the headpiece of container 21 and, with opened valve 7, is drawnoff from the bottom of the container 21 via tube a. This whole processis finished in a few seconds.

In FIG. 10, there is shown an embodiment of a backrinse, and aregenerating-and-wash column in a single unit construction. In acircular cylindrical container 90 there is centrally disposed in anaxial direction a column 91. The back-rinse process takes place in thelatter, whereby the resin is fed through an intake funnel 92. The backrinse will take place in the inner column 91. After the inflow of theregenerating agent via an opening 93 provided on the bottom of thecontainer 90, the resins will be regenerated and forwarded in the space94 between the inner column 91 and the outer container 90. The resin isdrawn off through an immersion tube 96 from which it flows to adischarge conduit 95. The rinse-and-transport water is led throughconduit 97 into the container 90. The diameter of the column 91 isgenerally the same as the radial distance be tween the confronting wallsof the column 91 and the container 90. This embodiment has the advantagethat it considerably reduces the space required by the backrinse,regenerating, and wash-column portions of the installation.

The above-described installations may be employed in a variety ofmanners:

For the entire desalination of water, in combination with a carbonicacid scrubber, weak and strong acid cation-exchangers and weak or strongbasic anionexchangers,

as a water softener whereby a regenerated exchange column functions as aneutral exchanger with salt spring water,

for decarbonization with eventually postcoupled carbonic acid degasingscrubber,

for treatment ol'surface water by means of absorbing resin,

as protection of post-coupled complete desalination installationsagainst humic acids,

for treatment of metallic salt solutions of all kinds,

for treatment and cleaning of chromium acid baths,

paladium baths, acid coating baths. for the recovery of noble metals,for the treatment of glavanic rinse water, for the circulation as wellas a flowthrough unpoisoning and neutralization treatment, as atenside-exchanger for the removal ofnon-ionic tensides in waterysolutions, as a selectiveexchanger for the removal of leftover metaltraces from fresh and waste water, for the treatment of whey, for thetreatment and removal of radioactive agents from fresh and waste water.

This installation takes substantially less space than the ones employingconventional ionexchange columns. There now follows a comparison:

EXAMPLE Based upon a content of 3 mval/l of salt. an output of 30 cbm/h,and a usable volume capacity/l exchange agent ofl mval.

With the conventional column process a volume of ion-exchange masses of4.220 1 is needed.

With the described continuously working installation: 850 l. arerequired.

Space required for conventional installation:

40 qm surface area 4 m height cbm constructed room.

The process of the present invention has the following requirements;

17 qm surface area 4 m height 68 cbm constructed room.

By means of the described optimal exploitation of the regeneratingchemicals, there is present a small counter-ion effect so that a degreeof purity can be attained which is not possible with conventionalinstallations. When connecting a strongly acid cation-exchangecarbonacid scrubber to a strongly basic anionexchanger, the following degreesof purity of the processed water were obtained:

efficiency l/AS sodium content 1 mg/l silicic acid content 0.1 mg/l Withthe conventional process this degree of purity can be reached only in amixing bed.

Since the transporting intervals with the described process are large,contrary to those of the previously known continuous or quasi-continuousworking installations, the wearing of the resin is relatively low. At acycle time of 15 minutes there are required only 96 unloads and loads ofthe exchange agents within a working time of 24 hours. Consequently,less of the resin is lost in the method and apparatus of the presentinvention as compared to prior continuously working installations whichhave a cycle time of about 3 minutes and consequently have about 500load changes within 24 hours.

Although the invention is illustrated and described with reference to aplurality of preferred embodiments thereof, it is to be expresslyunderstood that it is in no way limited to the disclosure of suchplurality of embodiments, but is capable of numerous modificationswithin the scope of the appended claims.

What is claimed is:

1. ln a system for the treatment of water solutions by means of ionexchange masses, wherein the ion exchange masses through which thesolutions flow are conducted in charges cyclically from a treatmentcontainer to a regeneration-and-wash column and in circulation arereturned to the treatment container, the improvement which comprises,

a backrinse container. a regeneration-and-wash column and a treatmentcontainer,

said containers and column each having top and bottom portions andinlets and outlets for the ion exchange masses,

conduit means operatively connected to the inlets and outlets of saidbackrinse container, regeneration-and-wash column and treatmentcontainer for conducting said ion exchange masses therebetween,

said conduit means comprising a first pipe connecting the outlet of saidtreatment container to the inlet of said backrinse container, a secondpipe connecting the outlet of said backrinse container to the inlet ofsaid regeneration-and-wash column, and a third pipe connecting theoutlelt of said regeneration-and-wash column to the inlet of saidtreatment container,

said regeneration-and-wash column and backrinse container having each atleast one immersion tube extending therein from their respective topportions,

the immersion tube in said regeneration-and-wash column being connectedto the top portion of said treatment container by said third pipe andthe immersion tube in said backrinse container being connected to theregeneration-and-wash column by said second pipe, said immersion tube insaid regeneration-and-wash column taking off an amount of ion exchangemass charge for conduction to the top portion of said treatmentcontainer the volume of which corresponds to the volume of ion exchangemass charge removed from said funnel-like bottom portion of saidtreatment container, said immersion tubes respectively extending withinsaid top portions of said backrinse container and regeneration-and-washcolumn to an extent which corresponds volumetrically to a charge of ionexchange mass, and

means for introducing untreated water solution into said treatmentcontainer,

means for removing clean water from said treatment container,

means for introducing and removing backrinse water in said back-rinsecontainer,

means for introducing and removing wash water in saidregeneration-and-wash column,

an inlet and outlet tube operatively mounted in the mid-region of saidregeneration-and-wash column for introducing a regeneration agenttherein,

a recirculating device operatively connected to said inlet tube andoutlet tube,

a conduit tube connecting said inlet and outlet tube,

a pump operatively mounted in said conduit tube for producing across-water flow in said mid-region of said regeneration-and-wash columnvia said inlet and outlet tube,

a cylindrical member forming part of said recirculation device and beingcoaxially mounted in said mid-region, said cylindrical member having diametrically opposite openings for the cross-water flow. I

2. A system according to claim 1 wherein the backrinse container as wellas the wash-and-regeneration column are formed as a single unit, saidunit having an outer container, an axially extending inner containerarranged within the outer container and extending to the vicinity of thebottom of the outer container and defining an annular spacetherebetween, the inner container forming the backrinse container andthe annular space between the inner and the outer containers forming theregeneration-and-wash column.

3. A system according to claim 1 wherein the regeneration-and-washcolumn is U-shaped.

4. A system according to claim 1 wherein the backrinse container has avolume such that it contains at least the volume of two ion-exchangemass charges.

5. A system according to claim 1, wherein both the upper and the lowerends of the treatment container are shaped conically.

6. A system according to claim 1, including a cleanwater reservoir, saidclean-water reservoir being combined with an untreated-water reservoir,and conduit means connecting said clean-water reservoir to said meansfor introducing back-rinse water and connecting said untreated-waterreservoir to said means for introducing untreated water solution, and adevice providing for the overflow of clean-water into the untreatedwaterreservoir.

1. IN A SYSTEM FOR THE TREATMENT OF WATER SOLUTIONS BY MEANS OF IONEXCHANGE MASSES, WHEREIN THE ION EXCHANGE MASSES THROUGH WHICH THESOLUTION FLOW ARE CONDUCTED IN CHARGES CYCLICALLY FROM A TREATMENTCONTAINER TO A REGENERATION-ANDWASH COLUMN AND IN CIRCULATION ARERETURNED TO THE TREATMENT CONTAINER, THE IMPROVEMENT WHICH COMPRISES, ABACKRINSE CONTAINER, REGENERATION-AND-WASH COLUMN AND A TREATMENTCONTAINER, SAID CONTAINERS AND COLUMN EACH HAVING TOP AND BOTTOMPORTIONS AND INLETS AND OUTLETS FOR THE ION EXCHANGE MASSES, CONDUITMEANS OPERATIVELY CONNECTED TO THE INLETS AND OUTLETS OF SAID BACKRINSECONTAINER, REGENERATION-AND-WASH COLUMN AND TREATMENT CONTAINER FORCONDUCTING SAID ION EXCHANGE MASSES THEREBETWEEN, SAID CONDUIT MEANSCOMPRISING A FIRST PIPE CONNECTING THE OUTLET OF SAID TREATMENTCONTAINER TO THE INLET OF SAID BACKRINSE CONTAINER, A SECOND PIPECONNECTING THE OUTLET OF SAID BACKRINSE CONTAINER TO THE INLET OF SAIDREGENERATION-AND-WASH COLUMN, AND A THIRD PIPE, CONNECTING THE OUTLET OFSAID REGENERATION-AND-WASH COLUMN TO THE INLET OF SAID TREATMENTCONTAINER, SAID REGENERATION-AND-WASH COLUMN AND BACKRINSE CONTAINERHAVING EACH AT LEAST ONE IMMERSION TUBE EXTENDING THEREIN FROM THEIRRESPECTIVE TOP PORTIONS, THE IMMERSION TUBE IN SAIDREGENERATION-AND-WASH COLUMN BEING CONNECTED TO THE TOP PORTION OF SAIDTREATMENT CONTAINER BY SAID THIRD PIPE AND THE IMMERSION TUBE IN SAIDBACKRINSE CONTAINER BEING CONNECTED TO THE REGENERATION-AND-WASH COLUMNBY SAID SECOND PIPE, SAID REGENER SION TUBE IN SAID REGENERATION-ANDWASH COLUMN TAKING OFF AN AMOUNT OF ION EXCHANGE MASS CHARGE FORCONDUCTION TO THE TOP PORTION OF SAID TREATMENT CONTAINER THE VOLUME OFWHICH CORRESPONDS TO THE VOLUME OF ION EX-
 2. A system according toclaim 1 wherein the backrinse container as well as thewash-and-regeneration column are formed as a single unit, said unithaving an outer container, an axially extending inner container arrangedwithin the outer container and extending to the vicinity of the bottomof the outer container and defining an annular space therebetween, theinner container forming the backrinse container and the annular spacebetween the inner and the outer containers forming theregeneration-and-wash column.
 3. A system according to claim 1 whereinthe regeneration-and-wash column is U-shaped.
 4. A system according toclaim 1 wherein the backrinse container has a volume such that itcontains at least the volume of two ion-exchange mass charges.
 5. Asystem according to claim 1, wherein both the upper and the lower endsof the treatment container are shaped conically.
 6. A system accordingto claim 1, including a clean-water reservoir, said clean-waterreservoir being combined with an untreated-water reservoir, and conduitmeans connecting said clean-water reservoir to said means forintroducing back-rinse water and connecting said untreated-waterreservoir to said means for introducing untreated water solution, and adevice providing for the overflow of clean-water into theuntreated-water reservoir.